Composition and method for treating and remediating aqueous waste streams

ABSTRACT

An apparatus for treating a stream of contaminated water having an elevated concentration of at least one of light metals, heavy metals, sulfates that includes at least one process fluid inlet communicating with a process conduit; at least one electrode reaction vessel in fluid communication with the process conduit, the reaction vessel having an interior chamber and at least one electrode positioned in the reaction chamber, the electrode powered by a alternating current source; and at least one magnetic field reaction vessel in fluid communication with the process conduit, the magnetic field reaction vessel having an outwardly oriented surface and an opposed inwardly oriented surface, the magnetic field reaction vessel having at least one magnet in contact with the inwardly oriented surface of the magnetic field reaction vessel.

The present application claims priority to pending U.S. provisionalapplication No. 62/354,556 filed Jun. 24, 2016, the disclosure of whichis incorporated by reference herein

BACKGROUND

The present invention pertains to methods and composition for treatingwaste and effluent waters originating from sources including but notlimited to manufacturing as well as excavation and mining operations.

Many times, water effluent is a necessary product of manufacturing andmining operations. The water effluent produced can include one or moretrace compounds that are dissolved or suspended in the process stream.Many of these trace compounds that are entrained in the process streamcan have deleterious or adverse effects if discharged into thesurrounding environment. Discharge of many such compounds is regulatedby various state, local and federal environmental agencies.

In operations such as mineral and energy extraction, copious amounts ofwater can sometimes be employed in various processes and sub processes.Typically, this water must be processed prior to discharge to reduce oreliminate process contaminants. In certain situations, such as mineralextraction operations, the extraction sites themselves, whether activeor inactive, provide a generation source as water from rain, storm waterrunoff and aquifer leaching carries various contaminants away from theoriginal extraction site into the surrounding environment. In miningoperations, this is generally referred to as Acid Mine Drainage (AMD) oracid rock drainage. Acid mine drainage results from oxidation of metalsulfide minerals such as pyrites and other ores. The various extractionsites can produce effluent that has elevated levels of one or more ofthe following metal contaminants, sulfur-containing compounds, volatileand dissolved organics. These contaminants can exist in either dissolvedor suspended for and can be present as ions or as compounds such ashigher oxidation state compounds.

Metal contaminants and metal compounds can include heavy metals and/orlight metals. Heavy metals include, but are not limited to, iron.copper, zinc, magnesium, manganese, aluminum, cadmium, nickel and lead,selenium, mercury, cobalt and the like. Sulphur containing compoundsinclude various sulfates, sulfides, and sulfites. Additionally, thewater material can contain various cyanides, cyanates and the like.

Past efforts have been directed to processes that can treat moderate tohigh concentrations of dissolved metals and sulfates, i.e. levels aboveabout 5000 ppm. In many processes, treatment technology employs avariety of tactics to precipitate metal contaminants and reduce sulfateand cyanate concentration. Unfortunate side effects of such processesinclude the precipitation of hazardous material as metal hydroxides andcalcium sulfate which results in significant disposal costs andnecessitates the use of hazardous and/or difficult-to-handle reagents.Additionally, the nature, quality and contaminant panel varies fromorigination site to origination site, making it difficult to provideremediation process and protocol that is efficient and effective acrossa variety of locations and situations.

It has been difficult to provide processes that adequately address andremediate the environmental challenges specific to each given generationsite. It would be desirable to provide a device and method that canaddress and mitigate various target compounds at a variety ofconcentration levels present in the specific effluent material such asmaterial associated with acid mine drainage. It would also be desirableto provide a device and method that can address and mitigate varioustarget compounds at various concentration levels in industrial processstreams.

SUMMARY

An apparatus is disclosed for treating a stream of contaminated waterthat includes at least one process fluid inlet communicating with aprocess conduit and at least one electrode reaction vessel in fluidcommunication with the process conduit. The reaction vessel has aninterior chamber and at least one electrode positioned in the interiorchamber. The electrode is powered by a pulsed electric current source.The apparatus also includes and at least one magnetic field reactionvessel that is in fluid communication with the process conduit. Themagnetic field reaction vessel has an outwardly oriented surface and anopposed inwardly oriented surface and has at least one magnet inphysical contact with the inwardly oriented surface of the magneticfield reaction vessel. The apparatus is useful for the treatment of anaqueous process stream having an elevated concentration of at least onetarget contaminant compound or component and can have specificapplicability in treatment of process streams in which the targetcompound component or component includes at least one of light metals,heavy metals, sulfates, cyanides and compounds and complexes thereof.

Also disclosed herein is a process for treating a stream of contaminatedwater having an elevated concentration of at least one target compoundcomponent or component. In certain embodiments, the target compoundcomponent can include at least one light metals, heavy metals, sulfates,cyanides, hydrocarbons, substituted hydrocarbons and compounds andcomplexes thereof. The process includes the step of charging the processstream with a quantity of a compound having the following formula:

$\lbrack {\frac{H_{x}O_{({x - 1})}}{2} + ( {H_{2}O} )_{y}} \rbrack Z$

wherein x is and odd integer ≧3, y is an integer between 1 and 20 and Zis a polyatomic ion, with Z being at least one of a Group 14 through 17monoatomic ion having a charge between −1 and −3 and/or a polyatomic ionhaving a charge between −1 and −3. The process also includes the step ofexposing the process stream to a pulsed electric field and to a focusedmagnetic field having a value between 10 gauss and 1,000,000 gauss.Exposure of the process stream to the pulsed electric field and thefocused magnetic field can occur in any order relative to one another.The steps of exposure and charging can occur in any order relative toone another.

BRIEF DESCRIPTION OF THE DRAWINGS

In the present disclosure reference is made to the following variousdrawings in which like reference numerals are used for like elementsthroughout the various figures. The drawing figures are for illustrativepurposes only and include the following:

FIG. 1 is a diagram of an embodiment of an apparatus for treating aprocess stream having at least one target contaminant; and

FIG. 2 is a process diagram outlining an embodiment of-processesassociated with further treatment of the aqueous material produced inthe method outlined in FIG. 1.

DETAILED DESCRIPTION

Disclosed herein is an apparatus and method for treating a stream ofcontaminated water. As broadly described, the apparatus includes atleast one process fluid inlet that communicates with a source ofcontaminated water in a manner that permits conveyance of at least aportion of the contaminated water into operative contact with theapparatus. As depicted in in FIGS. 4 and 5, this can be configured as atleast one process fluid inlet. The process conduit in a manner thatconveys at least a portion of the contaminated water into operativecontact with the apparatus. In certain embodiments, the device can beemployed to reduce and/or eliminate target contaminants. Non-limitingexamples of target chemical contaminant compounds that include at leastone of the following: metals, heavy metals, hydrocarbons, substitutedhydrocarbons, sulfate compounds and the like.

The device may include at least one electrolytic reaction vessel that isin fluid communication with the at least one process fluid conduit. Theelectrolytic reaction vessel has an interior chamber and at least oneelectrode operatively positioned in the reaction chamber that is poweredby an alternating current source. The electrolytic reaction vessel canbe configured to receive a volume of the process stream material andretain it in the electrolytic reaction vessel for an interval sufficientto permit process fluid exposure and interaction with the at least oneelectrode for a suitable contact interval. In certain embodiments, theinterval will be between 2 seconds and 90. minutes.

In certain embodiments, the apparatus can be configured to facilitatecontinuous through processing of the material in a continuous orsemi-continuous process flow as desired or required. In certainembodiments, the at least one electrode reaction vessel can beconfigured with a suitable internal volume to permit process fluidresidence sufficient to achieve contact between the process fluid andthe electrode for an interval between 2 seconds and 90 minutes per 100gallons of process fluid material. In certain embodiments, the intervalcan be between 5 seconds and 60 minutes per 100 gallons of process fluidmaterial. In certain embodiments, the contact interval can be between 10seconds and 30 minutes per 100 gallons of process fluid material;between 20 seconds and 30 minutes per 100 gallons of process fluidmaterial; between 15 seconds and 15 minutes per 100 gallons of processfluid material.

The pulsed electric field can be accomplished by one or more methodsincluding but not limited to at least one of the following: varyingvoltage intensity, varying the voltage delivery duration interval,varying the electrode polarity in at least one electrode that ispositioned in the electrolytic reaction vessel. The pulse frequency ratecan be between 60 per second to 1 per 10 minutes in certain embodiments.In other embodiments, it is contemplated that the pulse rate can bebetween 1 per second and 1 per minute, while in other embodiments, it iscontemplated that the certain embodiments, the pulse rate can be between1 per 5 seconds and 1 per minute. In certain embodiments, the pulsedelectric field is accomplished by polarity reversal in the electrode.

In certain embodiments, the at least one electrolytic reaction vesselcan be configured with at least one electrode. Where desired orrequired, the electrode can be configured as a bipolar electrode. Incertain embodiments, the at least one electrolytic reaction vessel willbe configured with at least one pair of electrodes positioned to provideanodic and cathodic exposure to the process fluid present in the atleast one electrolytic reaction vessel. It is also contemplated the atleast one electrode reaction vessel can include a plurality of electrodeassemblies if desired or required.

In the apparatus, as disclosed, the at least one electrolytic reactionvessel can be in electronic connection with a suitable control unit andcan include suitable regulators, interfaces and the like configured tosupply suitable pulsed electric current to the at least one electrode.

The at least one electrode can be configured to alternate or reversepolarity from anode to cathode in a pulsed or intermittent alternatemanner. It is contemplated that polarity of the subject anode can bereversed in an alternating manner. In certain embodiments, the polaritycan be reversed in a frequency at least between 60 reversals per secondand 1 reversal per 10 minutes. In certain embodiments, the frequency canbe between 1 reversal per second and 1 reversal per minute, while inother embodiments, the frequency can be between 1 reversal per 5 secondsand 1 reversal per minute. Without being bound to any theory, it isbelieved that the reversal in polarity can enhance electrode surfaceactivity and that exposure in the can provide the electrolytic reactionvessel can produce an induced charge state in the process fluid stream.

Without being bound to any theory, it is believed that exposure to theelectrode(s) promoted at least one electrochemical reaction on orproximate to the electrode surface that catalyzes chemical reaction thatbreak one or more bonds existing in compounds present as contaminant(s)in the aqueous process stream rendering them more amenable to subsequentreactive processing. It is believed that the process occurring at orproximate to the electrode surface ionizes compounds present in theassociated aqueous material.

The at least one electrode can be composed of any suitable material. Incertain embodiments, the electrode can be composed of a conductivematerial and can be either inert or reactive. Non-limiting examples ofinert materials suitable for use as an electrode can include one or moreof: carbon, graphite, gold, platinum, rhodium and the like. Non-limitingexamples of reactive electrode materials include copper, zinc, lead,silver and the like.

The apparatus may include at least one magnetic field region reactionvessel in fluid communication with the process fluid conduit. Themagnetic field region reaction vessel can be configured to expose theprocess fluid to a non-polar magnetic field. The magnetic field reactionvessel has an outwardly oriented surface and an opposed inwardlyoriented surface with at least one magnet in contact with the inwardlyoriented surface of the magnetic field reaction vessel. The magneticfield reaction vessel has at least one magnet that is in contact withthe inwardly oriented surface of the magnetic reaction vessel. Incertain embodiments, the magnet can be an electromagnet. In certainembodiments, the magnet material can be a rare-earth magnet.Non-limiting examples of suitable rare earth magnets are materials madefrom alloys of rare earth elements including those of the lanthanideseries plus scandium and yttrium. In certain embodiments, such magnetscan exert a magnetic field that exceeds 5000 to 10,000 gauss such as aneodynium magnets and sumarium-cobalt magnets.

In various embodiments, the magnetic field generated in the magneticfield region reaction vessel can be configured to provide a focusedmagnetic field having a magnetic flux value between 10 gauss and2,000,000 gauss. In certain embodiments, the magnetic field will bebetween 5000 and 1,000,000 gauss in certain applications and between5000 and 100,000 gauss. It is to be understood that in certainapplications, the magnetic field can be between 10 and 10,000 gauss.

It is contemplated that the process stream can be exposed to thegenerated magnetic field for an interval sufficient to induce magneticorientation of one or more molecules present in the process streamrelative to the generated field. In certain embodiments, the exposuretime can be an interval between 5 seconds and 90 minutes per 100 gallonsof process fluid material, while in other embodiments, it iscontemplated that this exposure interval is between 15 seconds and 10minutes per 100 gallons of process fluid material. Without being boundto any theory, it is believed that the indices molecular orientation canbe exhibited in water molecules present in the aqueous carrier itself incertain embodiments. In certain embodiments, the contact interval can bebetween 10 seconds and 30 minutes per 100 gallons of process fluidmaterial; between 20 seconds and 30 minutes per 100 gallons of processfluid material; between 15 seconds and 15 minutes per 100 gallons ofprocess fluid material.

The at least one magnetic field reaction vessel can be configured suchthat the aqueous process stream that traverses through it will have aresidence time sufficient to affect the magnetic alignment in theaqueous process stream material. In certain embodiments, it iscontemplated that the residence time will be between 15 seconds and 2hours with residence with residence times between 30 seconds and 1 hourin certain embodiments.

The device also includes at least one charge fluid introductionmechanism that is in fluid communication with the process fluid conduit.In certain embodiments, the charge fluid introduction conduit can belocated at a location that is upstream of at least one of the electrodereaction vessel and/or the magnetic field reaction vessel. Inembodiments of the device as disclosed the charge fluid can contain acompound having the following formula:

$\lbrack {\frac{H_{x}O_{({x - 1})}}{2} + ( {H_{2}O} )_{y}} \rbrack Z$

wherein x is and odd integer ≧3, y is an integer between 1 and 20 and Zis a polyatomic ion, with Z being at least one of a Group 14 through 17monoatomic ion having a charge between −1 and −3 and/or a polyatomic ionhaving a charge between −1 and −3.

The charge fluid conveying conduit can include suitable pumps, sensors,metering devices and the like as desired or required to control theintroduction of the charge fluid. The charge fluid conveying conduit canbe either permanently or releasably connected to the process fluidconduit at a suitable location. In certain embodiments, the charge fluidconveying conduit can be connected to the process fluid conveyingconduit at a location up stream of at least one of the at least oneelectrolytic reaction vessel, the at least one magnetic field regionreaction vessel or both. It is also contemplated that the device caninclude multiple charge fluid conveying conduits that are positioned atmultiple locations along the process fluid conveying conduit.

It is contemplated that the at least one charge fluid conveying conduit,the at least one electrolytic reaction vessel and the at least onemagnetic field region reaction vessel can be positioned along theprocess fluid conduit in any suitable sequence. In certain embodiments,at least one charge fluid conveying conduit will be oriented upstream ofthe at least one electrolytic reaction vessel and the at least onemagnetic field region reaction vessel. The at least one electrolyticreaction vessel and the at least one magnetic field region reactionvessel can be oriented in the process fluid conduit in any orderrelative to one another. In certain embodiments, at least oneelectrolytic reaction vessel can be positioned upstream of at the leastone magnetic field region reaction vessel.

In certain embodiments, the device can include at least two magneticfield region reaction vessels and at least two one electrolytic reactionvessels that are positioned in fluid contact with the process conduitsuch that the process stream is conveyed sequentially from residence inan electrolytic reaction vessel into a magnetic field region reactionvessel and from residence in the magnetic field region reaction vesselinto a at least one downstream electrolytic reaction vessel and fromthere into a downstream magnetic field region reaction vessel.

The method as disclosed herein is directed to treating an effluentstream having elevated levels of at least one target contaminant presentin an aqueous process stream. The target contaminant can be one or moreof the following: metals, heavy metals, sulfates, cyanides hydrocarbons,substituted hydrocarbons and compounds and complexes thereof.

The method as disclosed herein includes the steps of: collecting atleast a portion of aqueous process stream, exposing the collected streamto a pulsed electric field for an interval between about 15 seconds andabout 60 minutes; and exposing the collected fluid to a focused magneticfield, the magnetic field having a value between 10 gauss and 1,000,000gauss in certain applications.

In certain embodiments, the method is directed to a process or processesfor treating a stream of contaminated water reducing having an elevatedconcentration of at least one target compound component or component. Incertain embodiments, the process includes the step of charging theprocess stream with a quantity of a compound having the followingformula:

$\lbrack {\frac{H_{x}O_{({x - 1})}}{2} + ( {H_{2}O} )_{y}} \rbrack Z$

wherein x is and odd integer ≧3, y is an integer between 1 and 20 and Zis a polyatomic ion, with Z being at least one of a Group 14 through 17monoatomic ion having a charge between −1 and −3 and/or a polyatomic ionhaving a charge between −1 and −3.

The process also includes the step of exposing the process stream to apulsed electric field and to a focused magnetic field having a valuebetween 10 gauss and 1,000,000 gauss. Exposure of the process stream tothe pulsed electric field and the focused magnetic field can occur inany order relative to one another. The steps of exposure and chargingcan occur in any order relative to one another.

The effluent stream that is treated by the method and device asdisclosed herein can be an aqueous material derived from varioussources. The effluent stream will contain at least one targetcontaminant. In certain applications, the target contaminant can be atleast one of metals, heavy metals, sulfides and chlorides, hydrocarbons,substituted hydrocarbons as well as compounds and complexes thereof. Thetarget contaminant can exist as suspended solids, dispersed solids,dissolved solids and/or mixtures thereof. A used herein the term “heavymetals” is defined as dense metals and metalloids having a specificgravity that is at least five times that of water. Non-limiting examplesof such materials include chromium, cobalt, nickel, copper, silver,zinc, cadmium, mercury, thallium, lead, antimony, arsenic, selenium. Inother applications such as those associated with metal cleaning,treatment and processing, the target contaminant can be a material suchas monovalent transition metals, materials such as aluminum complexescontaining selenium, manganese, molybdenum and the like as well aschromium containing materials such as chromium nickel cadmium complexes,mercury containing compounds such as mercury lead compounds, preciousmetals such as silver and silver complexes, copper and copper containingcompounds such as copper-zinc materials. Other target materialsgenerated by industrial processes that can be treated by the process anddevice as disclosed herein include organic phosphate materials, organicsulfate materials organic nitrate materials, metal carbonates as well ascyanides, both free and complexed. Non-limiting examples of complexedcyanides include nitroprussides and material such as K₃FeCn₆.

The pulsed electric field to which the process stream is exposed can beaccomplished by exposing the process stream to a pulsed electric fieldcomprises the step of contacting the process stream with at least oneelectrode and varying at least one of varying at least one of voltageintensity, voltage delivery duration, electrode polarity in the at leastone electrode positioned in the electrolytic reaction vessel. The pulserate can be between 60 per second and 1 per ten minutes in certainembodiments, with rates between 1 per second and 1 per minute in certainembodiments, and 1 per 5 seconds and 1 per 1 minute in others.

Nonlimiting examples of suitable electrode material include variousinert or reactive conductive materials. Non-limiting examples of inertmaterials suitable for use as an electrode can include one or more of:carbon, graphite, gold, platinum, rhodium and the like. Non-limitingexamples of reactive electrode materials include copper, zinc, lead,silver and the like.

The aqueous process stream can remain in the pulsed electric field foran interval sufficient to permit reaction and generation of hydrogenion-water complexes. In certain embodiments, this interval can bebetween 2 seconds and 90 minutes per 100 gallons of process fluidmaterial. In certain embodiments, the interval can be between 5 secondsand 60 minutes per 100 gallons of process fluid material. In certainembodiments, the contact interval can be between 10 seconds and 30minutes per 100 gallons of process fluid material; between 20 secondsand 30 minutes per 100 gallons of process fluid material; between 15seconds and 15 minutes per 100 gallons of process fluid material.

The process as disclosed herein also include the step of exposing theaqueous process stream to a generated magnetic field of between 10 gaussand 2,000,000 gauss. In certain embodiments, the magnetic field will bebetween 5000 and 1,000,000 gauss in certain applications and between5000 and 100,000 gauss. It is to be understood that in certainapplications, the magnetic field can be between 10 and 10,000 gauss. Theprocess fluid can be exposed to the generated magnetic field for aninterval sufficient to induce magnetic orientation of one or moremolecules present in the process stream relative to the generated field.Without being bound to any theory, it is believed that exposure to thegenerated magnetic field, particularly when such exposure occurs afterthe exposure to the pulsed electric field, induces orientation of thehydration cages previously generated in the process fluid stream due toexposure to the pulsed electric field. In such embodiments, it iscontemplated that the interval between exposure to the pulsed electricfield and the generated magnetic field will be one sufficient tomaximize the concentration of hydration cages present in the processstream. In certain embodiments, this interval will be less than oneminute, while in others, the interval will be between 30 seconds and 3hours.

The interval during which the process fluid is exposed to the generatedmagnetic field will be between 5 seconds and 90 minutes per 100 gallonsof process fluid material in certain embodiments. In certainembodiments, the contact interval can be between 10 seconds and 30minutes per 100 gallons of process fluid material; between 20 secondsand 30 minutes per 100 gallons of process fluid material; between 15seconds and 15 minutes per 100 gallons of process fluid material.

The step of charging the process stream with a quantity of a compoundhaving the following formula:

$\lbrack {\frac{H_{x}O_{({x - 1})}}{2} + ( {H_{2}O} )_{y}} \rbrack Z$

wherein x is and odd integer ≧3, y is an integer between 1 and 20 and Zis a polyatomic ion, with Z being at least one of a Group 14 through 17monoatomic ion having a charge between −1 and −3 and/or a polyatomic ionhaving a charge between −1 and −3 can occur at any point in theaforementioned process. In certain embodiments, it is contemplated thatx is an integer between 3 and 12, while in others, it is contemplatedthat x is an integer between 3 and 9. In certain embodiments, it iscontemplated that y is an integer between 1 and 5. Suitable material canbe prepared by the steps outlined in US Application Number 2016-031209,the contents of which are incorporated herein. In certain embodiments,the compound can be selected from the group consisting of hydrogen (1+),triaqua-μ3-oxotri sulfate (1:1); hydrogen (1+), triaqua-μ3-oxotricarbonate (1:1), hydrogen (1+), triaqua-μ3-oxotri phosphate, (1:1);hydrogen (1+), triaqua-μ3-oxotri oxalate (1:1); hydrogen (1+),triaqua-μ3-oxotri chromate (1:1) hydrogen (1+), triaqua-μ3-oxotridichromate (1:1), hydrogen (1+), triaqua-μ3-oxotri pyrophosphate (1:1),and mixtures thereof.

In certain embodiments, the charging step well occur prior to theexposure to the pulsed electric field and/or the generated magneticfield. It is also within the purview of this disclosure that thecharging step occur at intervals before, between and/or during thesesteps. The compound can be present in an aqueous composition at aconcentration between 100 ppm and 1,000,000 ppm in the resulting chargedaqueous process fluid in certain embodiments. Where the compound isadded in divided dose through the process, it is contempered that thecharged aqueous process fluid can exhibit a concentration between 100ppm to 1,000,000 ppm after each charge addition.

Without being bound to any theory, it is believed that the presence ofthe charging compound in the aqueous process stream during one or bothof the electric field exposure step and/or the exposure to the focusedgenerated magnetic field contributes to the production of hydrationcages in the aqueous process stream. Additionally, it is believed thatthe presence of the charging compound produces an aqueous process fluidhaving elevated levels of available reactive molecular hydrogen which inturn reacts with at least one target contaminant both during theaforementioned steps and during downstream processing to producecompounds and chemical complexes that can be removed duringclarification and separation steps.

It is contemplated that the method and process as disclosed herein canbe used on its own or in combination with various other remediation andtreatment operations to produce remediated water with reduced levels oftarget material. The produced material may be appropriate for dischargeinto streams or waterways in certain applications. In other operation,the water produced may be amenable for subsequent treatment orprocessing.

It is also contemplated that the process and apparatus as defined hereincan be used to treat and remediate aqueous process streams generatedfrom one or more municipal or consumer generated processes, for exampletextile washing, laundry and light cleaning operations as well cleaningprocesses associated with operations such as washing vehicles et cetera,to produce potable and recycled water.

The resulting process water produced by the process and device asdisclosed herein have reduced levels of contamination sufficient topermit recycle and reuse closed loop industrial processing systems andeven use in use in non-agricultural irrigation applications to supportnon-food plant growth. In certain applications, based factors including,but not limited to, original contamination levels and/or the level ofprocessing intensity, the resulting aqueous stream can be suitable foruse in applications such as range grass watering for animal feed and thelike. In certain applications, the resulting aqueous material can beused for non-consumption human contact and even as potable drinkingwater in certain applications.

An embodiment of the process 10 for treating and remediating water asdisclosed herein is depicted in FIG. 1. The process as broadly construedis directed to exposing a process stream having at least one targetcontaminant to an electrolytic reaction environment and exposing theprocess stream to a magnetic field. These exposures can occursequentially in either order or iteratively in either order and canproceed in whole or in part simultaneously in certain instances. Asdepicted in FIG. 1, the process 10 includes a step in which the processstream having at least one target contaminant entrained therein into anelectrode reaction vessel as at reference numeral 20. The aqueous streamcan remain in the in the electrode reaction vessel for an intervalsufficient to permit reaction and generation of hydrogen ion-watercomplexes.

The process 10 also includes the step introducing the aqueous processstream into at least one magnetic field region reaction vessel as atreference numeral 30. The aqueous process stream can reside in thereaction vessel for an interval sufficient to affect the magneticalignment in the aqueous process stream material. The steps outlined atreference numerals 20 and 30 can be repeated iteratively or sequentiallyas desired or required.

Where desired or required process can also include the charging withsuitable base additives including but not limited to suitable stablehydronium type additive materials as desired or required. In certainembodiments, the stable base hydronium type additive materials caninclude one or more of the following:

a composition of matter having the following chemical structure:[H_(x)O_(x-y)]_(m)Z_(n)

where x is an integer greater than 3;

y is an integer less than x;

m is an integer between 1 and 6;

n is an integer between 1 and 3; and

Z is a monoatomic cation, polyatomic cation or cationic complex.

In certain embodiments, the stable base hydronium complex will be addedafter the steps of exposing the aqueous process stream to the pulsedelectric field and the focused magnetic field and in certain embodimentscan occur after removal of generated compounds such as sulfate solids.In certain embodiments, the stable hydronium compound can be added toprovide a solution concentration between 10 ppm and 50,000 ppm. Incertain embodiments, the stable hydronium additive will have theaforementioned formula in which Z is one of a monoatomic cation, apolyatomic ion or a cationic complex having a charge of +2 or greater inwhich at least a portion of the second compound is present as at leastone of H₄O₃ ²⁻, H₅O₂ ²⁻, H₇O₂ ²⁻, H₆O₅ ²⁻ and mixtures thereof incoordinated combination with working bridging ligands containing stablehydroxonium anion clusters in aqueous solution. Non-limiting examples ofsuch material are outlined in US Application Number 2016-034019, thedisclosure of which is incorporated herein by reference.

Referring now to the apparatus depicted in FIG. 2 there is illustrated aremediation system configured for addressing heavily contaminatedaqueous streams as may be generated by industrial manufacturingprocesses, mining operations and the like. The apparatus 50 includes atleast one aqueous process fluid inlet 52 configured to convey theaqueous process fluid to be treated from an exterior source into theapparatus 50.

The apparatus 50 also includes at least one electrolytic reaction vessel54 that is configured to introduce a charge into the aqueous stream andinduce a charged state in the aqueous material. The apparatus 50 alsoincludes at least one magnetic field region reaction vessel 56 that isconfigured to expose the process fluid to a non-polar magnetic fieldthat is sufficient to orient water molecules present in the aqueousprocess fluid. As depicted, the magnetic field region reaction vessel 56is positioned downstream of the electrolytic reaction vessel 54. It iswithin the purview of this disclosure that the order of the respectivevessels 54, 56 be switched. As depicted, the respective reaction vessels54, 56 are configured for single-pass processing, however, it is alsowithin the purview of this disclosure that the apparatus 50 can beconfigured to permit iterative recirculation though one or both of thereaction vessels 54, 56. It is also with in the purview of thisdisclosure that the apparatus 50 include more the one of either vessel.Where multiple vessels are employed, the various vessels can be orientedin parallel, in series or in various configuration utilizing bothorientations as desired or required.

The apparatus also includes at least one charge fluid introductiondevice 53 in fluid communication with the conduit 52.

Once processed, the treated aqueous process stream can be conveyedthrough a suitable transit pipe into at least one clarify unit. In theembodiment depicted, the apparatus 50 includes a metal clarifier unit 60that is configured to trigger precipitation of metals entrained in theprocess stream as metal hydroxide sludge. The metal hydroxide sludge canbe conveyed out of the metal clarifier unit 60 by a suitable conduitsuch as conduit 62 for further processing and for environmentally safedisposal.

In the apparatus depicted in FIG. 1, metal hydroxide sludge is conveyedto a dewatering unit 64 to separate solid material from the associatedwater by suitable processes such as gravity, pressure, centrifugation orthe like. The resulting solid material that is generated is in the forma metal hydroxide cake sludge 66 that can be recycled, processed ortransferred for disposal in an environmentally suitable manner. Thewater separated during this operation can be conveyed away from thedewatering unit 64 by any suitable means such as conduit 68. In theapparatus 50 as depicted, conduit 68 is in fluid connection with theinlet conduit 52 at a location upstream of one or more of the reactorunits 54, 56. As desired, the separated aqueous material can bereintroduced in the aqueous process stream in a suitable manner. Incertain applications, the separated process water can be metered intothe process stream in the inlet conduit 52 in a manner that permitscontrolled dilution of the process stream. The conduit 68 can beequipped with appropriate meters etc. (not shown).

The clarified process fluid can exit the metal clarifier unit 60 via asuitable conduit such as conduit 70. In the embodiment depicted in FIG.2, the aqueous process stream can be introduced into a sulfate removalclarifier 72 that is configured to generate sulfate and a insolublecalcium sulfate that can be removed via a suitable conduit 74 to beconveyed to the a suitable dewatering unit 76 to produce solid materialin the form of pure anhydrous calcium sulfate 78 that can be removed forsuitable post process applications. The aqueous filtrate produced in thedewatering process can be conveyed form the dewatering unit 76 by asuitable conduit 80.

To facilitate calcium sulfate formation, the apparatus can include asuitable means for acidifying the process stream. In the apparatus 50can include a suitable acidification reservoir 82 that is in fluidcommunication with the process stream at a location downstream of themetal clarifier unit 60. In the embodiment depicted, the acidificationunit 82 is connected to the process stream at a location in the conduit70 and can include suitable meters, feedback sensors and the like.

In certain embodiments, the acidification reservoir 82 can be configuredto permit the process fluid to be admixed with volumes of an aqueousmaterial that includes a compound having the general formula:

$\lbrack {\frac{H_{x}O_{({x - 1})}}{2} + ( {H_{2}O} )_{y}} \rbrack Z$

-   -   wherein x is and odd integer ≧3, with x being an integer between        3 and 12 in certain embodiments and between 3 and 9 in certain        embodiments;    -   y is an integer between 1 and 20, with y being an integer        between 1 and 5 in certain embodiments; and    -   Z is a polyatomic ion, with Z being one of a group 14 through 17        monoatomic ion having a charge between −1 and −3 or a poly        atomic ion having a charge between −1 and −3

The clarified process stream that exits the clarification unit 72 into asuitable conduit 82 that communicates with a suitable storage anddistribution tank 84. It is contemplated that a portion of the processfluid accumulated in the storage and distribution tank 84 can be removedinto conduit 86 where it can be reintroduced into the initial processstream to achieve dilution and priming prior to entry into the reactors54, 56. The balance of the processed material can be conveyed into thesuitable pH neutralization tank 86 where the process stream can beneutralized as required and the material can be released as finaltreated effluent.

Without being bound to any theory, it is believed that the process andapparatus disclosed herein serves to break the chemical bonds betweencontaminants and water molecules by changing their valence state, whichallow metals to precipitate out of solution, forming insoluble metalprecipitants producing a treated effluent at between 6 and 10 pH. Thisprocess is capable of treating water to State and Federal dischargestandards, producing relatively small amounts of metal cake material,and is accomplished without generating large quantities of sludge. Thesystem has a simple design and a relatively small footprint, fail safemonitoring technology, minimal electrical requirements, minimalmaintenance and operational costs, high throughput, and is capable ofcontinuous operation.

It is believed that the system functions with minimal amounts ofnon-hazardous, non-toxic, non-corrosive, proprietary chemistriescompared to conventional hazardous slack lime. Minimal amounts ofnon-hazardous, food grade, GRAS-rated lime slurry are employed comparedto conventional hazardous slack lime with up to 50% decrease in sludgeproduction; producing a sludge that is free of heavy metals and otherdesirable material as well as production of material such as reclaimablemetal and materials such as calcium sulfate for use in post-processindustrial procedures such as the manufacture of metal free gypsum.

In order to further illustrate the present disclosure, reference is madeto the following non-limiting examples.

Example I

The process and an embodiment of the apparatus as disclosed herein isemployed on two samples taken from Cement Creek Colorado. Aftertreatment, levels of key metals were determined. The results aresummarized in TABLE I.

TABLE 1 Contaminant Sample Sample Treated Treated Federal drinking mg 12 1 2 water standards Aluminum 11 11 ND 0.23 N/A Cadmium 0.031 0.032 NDND 0.005 Copper 1.6 1.6 0.055 0.035 1.3 Iron 23 21 1.8 1.6 N/A Manganese18 18 11 7.9 N/A Lead 0.043 0.035 ND ND 0 Zinc 12 11 0.27 ND 5

Example II

Effluent from a chemical processing and surface engineering company wastreated according to the process as disclosed herein. The effluentincluded cadmium, nickel copper, gold, silver zinc, mercury and lead aswell as inorganic ligands that were treated and included free and totalcyanide, phosphates, and fluoride compounds. Organics included methylethyl ketone, acetone, and trichloroethylene. The process was evaluatedagainst incumbent treatment systems in place in the installation. It wasfound that the water discharged after treatment according to the processoutlined in the present disclosure had a water quality similar todistilled water and was able to meet the requirement for total toxicorganics. This was achieved with a 90% reduction in solid wastegenerated with treatment proceeding without reactivity, outgas sing orexothermicity.

While the invention has been described in connection with certainembodiments, it is to be understood that the invention is not to belimited to the disclosed embodiments but, on the contrary, is intendedto cover various modifications and equivalent arrangements includedwithin the spirit and scope of the appended claims, which scope is to beaccorded the broadest interpretation so as to encompass all suchmodifications and equivalent structures as is permitted under the law.

What is claimed is:
 1. An apparatus for treating a stream ofcontaminated water having an elevated concentration of at least onetarget chemical component, the apparatus comprising: at least oneprocess fluid inlet communicating with a process fluid conduit, theprocess fluid inlet in at least temporary fluid communication with asource of contaminated water having an elevated concentration of atleast one target chemical component, the target chemical componentselected from the group consisting of light metals, heavy metals,sulfates, hydrocarbons and mixtures thereof; at least one electrolyticreaction vessel in fluid communication with the process fluid conduit,the electrolytic reaction vessel having an interior chamber and at leastone electrode positioned in the interior chamber of the reaction vessel,the electrode powered by a pulsed electric current source; and at leastone magnetic field region reaction vessel, the magnetic field reactionvessel being in fluid communication with the process fluid conduit, themagnetic field reaction vessel having an outwardly oriented surface andan opposed inwardly oriented surface, the magnetic field reaction vesselhaving at least one magnet in contact with the inwardly oriented surfaceof the magnetic field reaction vessel.
 2. The apparatus of claim 1further comprising at least one electrode power regulation mechanism,the electrode power regulation mechanism configured to vary at least oneof voltage intensity, voltage delivery duration, electrode polarity inthe at least one electrode positioned in the electrode reaction vessel.3. The apparatus of claim 2 wherein the magnetic field reaction vesselis configured to exposing the aqueous process stream to a focusedmagnetic field having a value between 10 gauss and 100,000 gauss.
 4. Theapparatus of claim 1 further comprises at least one charging inlet, thecharging inlet configured to convey a metered quantity of an aqueouscomposition comprising a compound having the following formula:$\lbrack {\frac{H_{x}O_{({x - 1})}}{2} + ( {H_{2}O} )_{y}} \rbrack Z$wherein x is and odd integer ≧3, y is an integer between 1 and 20 and Zis a polyatomic ion, with Z being at least one of a Group 14 through 17monoatomic ion having a charge between −1 and −3 and/or a polyatomic ionhaving a charge between −1 and −3.
 5. The apparatus of claim 3 furthercomprising at least one separation device located downstream of the atleast one electrolytic reaction vessel and the at least one magneticfield region reaction vessel.
 6. The apparatus of claim 5 wherein theseparation device is at least one of a filtration unit, a centrifugeand/or a compressor.
 7. The apparatus of claim 1 comprising: at leastone electrode power regulation mechanism, the electrode power regulationmechanism configured to vary at least one of voltage intensity, voltagedelivery duration, electrode polarity in the at least one electrodepositioned in the electrode reaction vessel; and at least one charginginlet, the charging inlet configured to convey a metered quantity of anaqueous composition comprising a compound having the following formula:$\lbrack {\frac{H_{x}O_{({x - 1})}}{2} + ( {H_{2}O} )_{y}} \rbrack Z$wherein x is and odd integer ≧3, y is an integer between 1 and 20 and Zis a polyatomic ion, with Z being at least one of a Group 14 through 17monoatomic ion having a charge between −1 and −3 and/or a polyatomic ionhaving a charge between −1 and −3; and at least one controllerconfigured monitor characteristic of the process fluid, wherein themagnetic field reaction vessel is configured to exposing the aqueousprocess stream to a focused magnetic field having a value between 10gauss and 100,000 gauss.
 8. A method for reducing concentration of atleast one target contaminant in an aqueous process stream, the methodcomprising the steps of: charging the process stream with a quantity ofa compound having the following formula:$\lbrack {\frac{H_{x}O_{({x - 1})}}{2} + ( {H_{2}O} )_{y}} \rbrack Z$wherein x is and odd integer ≧3, y is an integer between 1 and 20 and Zis a polyatomic ion, with Z being at least one of a Group 14 through 17monoatomic ion having a charge between −1 and −3 and/or a polyatomic ionhaving a charge between −1 and −3; and at least one of the followingsteps: a) exposing the process stream to a pulsed electric field; b)exposing the process stream to a focused magnetic field having a valuebetween 10 gauss and 1,000,000 gauss.
 9. The method of claim 8 whereinthe process comprises the steps of sequentially: charging the processstream with a quantity of a compound having the following formula:$\lbrack {\frac{H_{x}O_{({x - 1})}}{2} + ( {H_{2}O} )_{y}} \rbrack Z\text{:}$exposing the aqueous process stream to a pulsed electric field; exposingthe aqueous process stream to a focused magnetic field having a valuebetween 10 gauss and 100,000 gauss.
 10. The method of claim 9 whereinthe target contaminant is at least one of metals, heavy metals, sulfidesand chlorides, hydrocarbons, substituted hydrocarbons as well ascompounds and complexes thereof.
 11. The method of claim 8 wherein thestep of exposing the process stream to a pulsed electric field comprisesthe step of contacting the process stream with at least one electrodeand varying at least one of varying at least one of voltage intensity,voltage delivery duration, electrode polarity in the at least oneelectrode positioned in the electrolytic reaction vessel.
 12. The methodof claim 10 wherein the process stream is exposed to the pulsed electricfield for an interval between 2 second and 90 minutes and where in thepulsing is do at least in part to varying electrode polarity.
 13. Themethod of claim 8 wherein the charging compound is selected from thegroup consisting of hydrogen (1+), triaqua-μ3-oxotri sulfate (1:1);hydrogen (1+), triaqua-μ3-oxotri carbonate (1:1), hydrogen (1+),triaqua-μ3-oxotri phosphate, (1:1); hydrogen (1+), triaqua-μ3-oxotrioxalate (1:1); hydrogen (1+), triaqua-μ3-oxotri chromate (1:1) hydrogen(1+), triaqua-μ3-oxotri dichromate (1:1), hydrogen (1+),triaqua-μ3-oxotri pyrophosphate (1:1), and mixtures thereof.
 14. Themethod of claim 13 further comprising the step of charging the processstream with a composition having the following chemical structure:[H_(x)O_(x-y)]_(m)Z_(n) where x is an integer greater than 3; y is aninteger less than x; m is an integer between 1 and 6; n is an integerbetween 1 and 3; and Z is a monoatomic cation, polyatomic cation orcationic complex.